• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A metallurgical plant has an upstream plant (7) in the production process for steel of a steelmaking plant (8) and a gas generating plant (1) which generates an export gas (2). In the export gas (2) contained carbon dioxide and / or water is at least partially removed from the export gas (2) in a separation device (3). A product gas (4) resulting therefrom is heated in a firing device (6) by burning a heating gas (11) before being fed to the upstream installation (7). The heating gas (11) is supplied to the firing device (6) to an extent which is considerably greater than is required for heating the product gas (4). The thermal energy produced when the heating gas (11) is burned is used thermally unless it is used for heating the product gas (4). The use can take place within the firing device (6) by generating steam and / or with respect to the gas flow of the flue gas (12) arising during combustion of the heating gas (11) behind the firing device (6). In the latter case, the use by preheating the hot gas (11) and / or by preheating a combustion gas used for burning the (11) oxidizing gas (10) and / or by the preheating and / or drying of the upstream plant (7) and / or the gas generating plant (1) supplied raw materials (20, 21) take place.
    公开号:AT511243A1
    申请号:T368/2011
    申请日:2011-03-17
    公开日:2012-10-15
    发明作者:Robert Dipl Ing Millner；Gerald Dipl Ing Rosenfellner
    申请人:Siemens Vai Metals Tech Gmbh；
    IPC主号:
    专利说明:

    1 '1' ♦ * 200811545
    Description: The present invention relates to an operating method for a metallurgical plant which has a plant upstream of the steel production plant in the steelmaking plant manufacturing process and a gas generating plant generating an export gas, - carbon dioxide and / or water contained in the export gas a separation device is at least partially removed from the export gas and a resulting product gas is heated by supplying a heating gas before being supplied to the upstream installation in a firing device. 15
    The present invention further relates to a metallurgical plant, which is designed such that it carries out such an operating method during operation. Such metallurgical systems and the associated operating methods are well known. IDNR: 2443 / V: 03-1.01 / B: Val
    In metallurgical plants, in particular in installations of the iron and steel producing industry, large quantities of heat energy are required at high temperatures. In such systems therefore fall large amounts of waste heat. The resulting waste heat is already partially used to preheat within the metallurgical plant resulting or to be processed intermediates - especially process gases. Even 30, the waste heat is already partially used to over a
    Steam generator and subordinate turbine to operate an electric generator.
    The object of the present invention is to create possibilities for making more efficient use of a metallurgical plant of the type mentioned in the introduction. 200811545 «* * * *» • «* · · ·
    The object is achieved by an operating method with the features of claim 1. Advantageous embodiments of the operating method according to the invention are the subject of the dependent claims 2 to 11.
    According to the invention, an operating method for a metallurgical system of the type mentioned in the design, - that the heating gas is supplied to the firing device to an extent that is considerably greater than is required for heating the product gas, - wherein the combustion of the fuel gas resulting thermal Energy, as far as it is not used for heating the product gas, within the firing device for the steam generation and / or with respect to the gas stream of the flue gas produced during combustion of the heating gas behind the firing device for preheating the hot gas and / or for preheating one for burning the hot gas used oxidizing gas and / or for the preheating and / or drying of the upstream plant and / or the gas generating plant to be supplied raw materials used thermally.
    In a preferred embodiment of the present invention, the flue gas produced during combustion of the heating gas is first used for steam generation and only then for heating the product gas.
    In some cases, it is necessary to keep the temperature of the product gas substantially constant at a set temperature. If this is the case and the temperature of the flue gas is too high, it is possible to add cold air to the flue gas after use to generate steam and before heating the product gas for temperature adjustment of the flue gas heating the product gas.
    In a particularly preferred embodiment of the present invention, it is provided that: 200811545 · * · ♦ · I · * * * ·
    • the heating of the product gas is limited to an intermediate temperature below a reaction temperature required for the use of the product gas in the upstream installation, although the thermal energy required for burning the heating gas is obtained, and that heated product gas is heated by a partial oxidation of the product gas from the intermediate temperature to the reaction temperature.
    If the thermal energy of the flue gas is sufficiently high, it is possible that the thermal energy of the flue gas behind the firing device is used to heat a thermal oil.
    It is possible that a portion of the export gas generated by the gas generating plant is used as the heating gas. Alternatively or additionally, it is possible for a process gas which accumulates during removal of the carbon dioxide and the water from the export gas and is enriched with carbon dioxide and water to be used as the heating gas. If the said process gas does not burn stable enough or does not contain the required thermal energy, the process gas can be admixed with another combustible gas or the process gas can be burnt together with the further combustible gas.
    The amount and / or the composition of the resulting export gas and, associated therewith, the amount and / or the composition of the resulting process gas are often subject to considerable fluctuations over time. In many cases, it may therefore be useful for the part of the export gas used as heating gas or the process gas to be temporarily stored in a low-pressure gas accumulator upstream of the firing device.
    In many cases, a combustible gas is produced during operation of the upstream plant. It is possible that the combustible gas is at least partially admixed with the export gas. Alternatively or additionally, the combustible gas can be used as the heating gas. In particular, if appropriate, the last-mentioned combustible gas can be added to the abovementioned process gas enriched with carbon dioxide and water or burnt together with this process gas.
    It is also possible that the operation of the upstream plant is a hot top gas. In this case, it is possible for the thermal energy contained in the top gas to be used for preheating the product gas before it is fed to the firing device and / or for the steam generation. The hot top gas may alternatively be a combustible or non-combustible gas.
    The upstream plant can be designed, for example, as a blast furnace, as a smelting reduction plant, as a smelting unit or as a direct reduction plant. The gas generating plant can be designed, for example, as a coal gasification plant or as a metal melting plant, in particular as an iron melting plant or as a smelting reduction plant.
    The object is further achieved by a metallurgical system with the features of claim 12. It is provided according to the invention to design a metallurgical installation of the type mentioned in the introduction by carrying out an operating method according to the invention during operation.
    Further advantages and details will become apparent from the following description of exemplary embodiments in conjunction with the drawings. 1 shows schematically a metallurgical plant, FIG. 2 shows schematically a detail of the metallurgical technique
    FIG. 1 schematically shows a possible embodiment of the technical facility of FIG. 1. FIG.
    According to FIG. 1, a metallurgical plant has a gas generating plant 1. The gas generating plant 1 can, for example, be used for the production of gas.
    It may be designed as a coal gasification plant or as a metal smelting plant. In the case of training as a metal melting plant, this can be designed in particular as an iron melting plant - also as a blast furnace, in particular oxygen blowing furnace - or as a smelting reduction plant. An oxygen blowing furnace is a blast furnace in which technically pure oxygen is used as hot blast and the resulting blast furnace gas can be recycled to the blast furnace.
    The gas generating plant 1 generates a gas 2 during operation, hereinafter referred to as export gas 2. The export gas 2 contains flammable components as well as additional carbon dioxide, water and, as a rule, nitrogen. The presence of carbon dioxide and water is indicated in FIG. 1 by the fact that in the case of the export gas the additives "CO2 " and "H20" stand.
    The export gas 2 is - completely or partially - fed to a separation device 3. In the separation device 3, the export gas 2 - possibly only the separation device 3 supplied part of the export gas 2 - processed. In particular, the carbon dioxide contained in the export gas 2 and / or the water contained in the export gas 2 are completely or partially removed from the export gas 2 in the separation device 3. This results in a product gas 4, in which compared to the export gas 2 carbon dioxide and water are depleted. This is indicated in FIG. 1 by the additions "C02- " and ,, H20- " indicated. On the other hand results in a process gas 5 - often referred to as tail gas - in which carbon dioxide and / or water are enriched. This is shown in FIG. 1 by the additions "CO2 +". and "H20 +" indicated.
    The product gas 4 is first fed to a firing device 6 and from there to a upstream plant 7. The upstream plant 7 is a plant that is upstream in the steel production process of a steelmaking plant 8. The upstream plant 7 can be designed, for example, as a blast furnace, as a smelting reduction plant, as a smelting unit or as a direct reduction plant. 200811545 ♦ * ♦ ·
    In the firing device 6, the product gas 4 is heated in a product gas heat exchanger 9. The chemical composition of the product gas 4 remains - at least 5 essentially - unchanged. Only the temperature of the product gas 4 changes.
    When firing the firing device 6, a heating gas 11 is burned into a flue gas 12 in the firing device 6 using an oxidizing gas 10 10. Both gases 10, 11 are supplied to the firing device 6. The oxidizing gas 10 may be, in particular, normal air.
    The heating gas 11 is supplied to the firing device 6 in a Um-15 catch, which is considerably larger than is required for heating the product gas 4. The firing device 6 therefore generates a considerable amount of excess thermal energy. The resulting thermal energy, as far as it is surplus - that is not needed and used for heating 20 of the product gas 4 -, for example, be used to generate within the firing device 6 by means of an evaporator 13 steam and so a water-steam cycle operate. For example, the steam may drive a turbine 14, which in turn drives an electric generator 15. Alternatively, the steam can be used elsewhere.
    If steam generation takes place, the evaporator 13 -see particularly clearly FIG. 2 -is arranged upstream of the product gas heat exchanger 9 with respect to the gas flow 30 of the flue gas 12. The resulting during combustion of the fuel gas 11 flue gas 12 is therefore initially used for steam generation and only then for heating the product gas 4. Optionally, by means of the flue gas 12, an overheating of the generated steam can take place. A possible superheater (not shown in the FIG) is in this case the product gas heat exchanger 9, possibly also the evaporator 13 in 200811545 ♦ · · «· ♦ · ♦
    ♦ ♦ ♦ «·« · · ·
    Reference to the gas flow of the flue gas 12 upstream. Furthermore, a preheating of the water to be evaporated can take place. A corresponding preheater (not shown in the FIG) is in this case arranged downstream of the product gas heat exchanger 9 in relation to the gas flow of the flue gas 12.
    Alternatively or in addition to a use for steam generation, it is possible to use the flue gas 12 in units 16 to 19, which are arranged with respect to the gas flow of the flue gas 12 behind the firing device 6.
    For example, the heating gas 11 can be preheated in a heating gas heat exchanger 16. Alternatively or in addition to the preheating of the heating gas 11, the oxidizing gas 10 can be preheated in an oxidizing gas heat exchanger 17. The preheating of the heating gas 11 and / or the oxidizing gas 10 takes place, of course, before supplying the said gases 10, 11 to the firing device 6.
    Furthermore, as an alternative or in addition to preheating the heating gas 11 and / or the oxidizing gas 10, a drying and / or preheating of raw materials 20 can take place in a raw material preparation device 18, which are to be supplied to the upstream unit 7. In an analogous manner, in a further raw material processing device 19 - additionally or alternatively - a drying and / or preheating of raw materials 21 take place, which are to be supplied to the gas generating plant 1. In particular, iron ore or coking coal are suitable as raw materials 21.
    If, in addition, excess thermal energy of the flue gas 12 is available, it is additionally possible to use the thermal energy of the flue gas 12 behind the firing device 6 in an oil heat exchanger 23 for heating a thermal oil 24.
    In some cases, it may be useful to adjust the temperature of the flue gas 12 heating the product gas 4. For this purpose, cold air 25 can be added to the flue gas 12 according to FIG. The admixing of the cold air 25 takes place in this case after the use of the flue gas 12 for generating steam, but - of course - before the heating of the product gas. 4
    It is possible to heat the product gas 4 in the firing device 6 up to a reaction temperature T (of generally more than 800 ° C.) which the product gas 4 must have in order to be used in the upstream plant 7. In many cases, however, it is advantageous to limit the heating of the product gas 4 to an intermediate temperature T ', which is below the reaction temperature T. This is true even though the burning of the fuel gas 11, the thermal energy required for this (ie for heating up to the reaction temperature T) is obtained. The intermediate temperature Τ 'may, for example, be about 400 ° C to about 600 ° C. If the product gas 4 in the firing device 6 is only heated up to the intermediate temperature Τ ', the product gas 4 heated in the firing device 6 is cooled as shown in FIG. 2 by partial oxidation of the product gas 4 in an oxidation device 26 from the intermediate temperature T' to the reaction temperature T. heated. As a rule, an oxidizing gas 27 is supplied to the oxidation device 26 for this purpose in addition to the product gas 4, for example technically pure oxygen {oxygen content at least 90%).
    The heating gas 11, which is burned in the firing device 6, can be chosen arbitrarily in principle. It is possible to supply the heating gas 11 of the metallurgical plant from the outside. Alternatively, the heating gas 11 may be a gas generated within the metallurgical plant. For example, it is possible for a portion of the export gas 2 generated by the gas generating plant 1 to be used as the heating gas 11 according to FIG. 3. Alternatively or additionally, it is possible that the process gas 5 is used as the heating gas 11. If necessary, the process gas 5 may be admixed with another combustible gas 28, another combustible gas 28. Alternatively, as far as necessary, the further combustible gas 28 can be burned in a separate burner of the firing device 6 together with the process gas 5.
    If a part of the export gas 2 or the process gas 5 is used as the heating gas 11, a low-pressure gas reservoir 29 is preferably arranged in the supply line of the corresponding gas 2, 5 to the firing device 6. The low-pressure gas accumulator 29 serves to compensate for fluctuations in quantity and / or composition which occur during the generation of the export gas 2 and / or the process gas 5. In the low-pressure gas reservoir 29, there is a gas pressure p, which is slightly greater than the atmospheric pressure.
    In many cases falls during operation of the upstream plant 7, a gas 30, which is hot and / or flammable. This gas 30 is often referred to as top gas 30. When the top gas 30 is combustible, it is possible to mix the top gas 30 - completely or partially - with the export gas 2. Alternatively or additionally, it is possible to use the top gas 30 as the heating gas 11. Optionally, use may be made together with the export gas 2 and / or the process gas 5. In particular, the top gas 30 may in this case be identical to that combustible gas 28 which is added to the process gas 5 or burned together with it.
    When the top gas 30 is hot, it is possible to use the thermal energy contained in the top gas 30 to preheat the product gas 4 before it is supplied to the firing device 6 and / or for steam generation (including possibly overheating). This is also indicated by dashed lines in FIG.
    The present invention has many advantages. In particular, an efficient use of the resulting thermal energy in the metallurgical plant and the resulting combustible gases is possible in a relatively simple manner. 200811545 • t · · ·
    • »» * • M (Φ • * 4 # «· ·«
    The above description is only for explanation of the present invention. The scope of the present invention, however, is intended to be determined solely by the appended claims. 200811545: 25 «i ι
    Reference sign list 1 2 3 4 5 6 7 8 9 10, 27 11 12 13 14 15 16 to 19 16 17 18, 19 20, 21 23 24 25 26 28 29 30
    Gas generation plant
    export gas
    separation device
    product gas
    process gas
    Befeuerungseinrichtung upstream facility
    Steelmaking plant
    Product gas Wärmetauseher
    oxidizing gases
    heating gas
    flue gas
    Evaporator
    turbine
    generator
    Aggregate
    Hot gas heat exchanger
    Oxidizing gas heat exchanger
    Raw material processing facilities
    Raw materials oil heat exchanger
    thermal oil
    cold air
    Oxidation device Further combustible gas Low-pressure gas reservoir Topgas p Gas pressure T Reaction temperature T 'Intermediate temperature
    权利要求:
    Claims (12)
    [1]
    200811545 1 · 1 ····················································································································································································································································································· (2) generating gas generating plant (1), - in the export gas (2) contained carbon dioxide and / or water in a separation device (3) is at least partially removed from the export gas (2) and thereby resulting product gas (4) before the Supply to the upstream plant (7) in a firing device (6) by burning a hot gas (11) is heated, - wherein the heating gas (11) of the firing device (6) is supplied in an amount which is considerably greater than for heating the product gas (4) is required, - in which the thermal energy produced when burning the heating gas (11), unless it is used for heating the product gas (4), is within the Firing device (6) for steam generation and / or with respect to the gas flow of the flue gas (12) produced during combustion of the heating gas (11) behind the firing device (6) for preheating the heating gas (11) and / or for preheating one for burning Heating gas (11) used oxidation gas (10) and / or for the preheating and / or drying of the upstream plant (7) and / or the gas generating plant (1) to be supplied raw materials (20, 21) is used thermally.
    [2]
    2. Operating method according to claim 1, characterized in that the burning of the fuel gas (11) resulting flue gas (12) is first used for steam generation and only thereafter for heating the product gas (4).
    [3]
    3. Operating method according to claim 2, characterized in that the temperature setting of the product gas (4) heating the flue gas (12) the flue gas (12) after use for * · 200811545 1¾

    Steam generation and before the heating of the product gas (4) cold air (25) is admixed.
    [4]
    4. Operating method according to claim 1, 2 or 3, characterized in that - the heating of the product gas (4) to an intermediate temperature (Τ ') below a for the use of the product gas (4) in the upstream plant (7) required reaction temperature ( T) is limited, although the combustion of the fuel gas (11), the required thermal energy is obtained, and - that the heated product gas (4) by a partial oxidation of the product gas (4) from the intermediate temperature (Τ ') to the reaction temperature (T ) is heated.
    [5]
    5. Operating method according to one of the above claims, characterized in that the thermal energy of the flue gas (12) behind the firing device (6) for heating a thermal oil (24) is used.
    [6]
    6. Operating method according to one of the above claims, characterized in that as heating gas (11) a part of the gas generating plant (1) generated export gas (2) and / or on removal of the carbon dioxide and water from the export gas (2) accumulating , Process gas enriched with carbon dioxide and water (5) - the latter possibly with the addition of a further combustible gas (28) or with burning together with the further combustible gas (28) - is used.
    [7]
    7. Operating method according to claim 6, characterized in that the heating gas used as (11) used part of the export gas (2) or the process gas (5) in one of the firing device (6) upstream low pressure gas storage (29) is cached. 12. ' 200811545
    [8]
    8. Operating method according to one of the above claims, characterized in that during operation of the upstream plant (7) a combustible gas (30) accumulates and that the combustible gas ^ [30] is at least partially admixed to the export gas (2) and / or as Heating gas (_11). is used.
    [9]
    9. Operating method according to one of the above claims, characterized in that during operation of the upstream plant (7) a hot top gas (30) is obtained and that in the top gas (30) contained thermal energy for preheating the product gas (4) prior to its supply to Firing device (6) and / or used for steam generation.
    [10]
    10. Operating method according to one of the above claims, characterized in that the upstream plant (7) is designed as a blast furnace, as a smelting reduction plant, as a melting unit or as a direct reduction onsanlage.
    [11]
    11. Operating method according to one of the above claims, characterized in that the gas generating plant (1) is designed as a coal gasification plant or as a metal melting plant, in particular as an iron melting plant or as a smelting reduction plant.
    [12]
    12. Hüttentechnische plant, which is designed such that it executes an operating method according to one of the above claims during operation.
    类似技术:
    公开号 | 公开日 | 专利标题
    AT507525B1|2010-09-15|METHOD AND DEVICE FOR OPERATING A MELT REDUCTION PROCESS
    DE2703921A1|1978-08-10|PROCEDURE FOR CARRYING OUT PARTIAL OXIDATION OF LIQUID AND / OR SOLID FUELS
    AT511243B1|2013-01-15|HÜTTENTECHNISCHE ANLAGE WITH EFFICIENT DOWNWATER USE
    DE102014203039A1|2015-08-20|Method and device for separating exhaust gas during the combustion of certain metals
    EP2984053A1|2016-02-17|Plant for producing cement clinker with gasification reactor for difficult fuels
    EP2844849A2|2015-03-11|Method for using the exhaust gases from plants for raw iron manufacture for generating steam
    DE19536383C2|2001-09-13|Method and device for the gasification of low calorific value fuels
    WO1985000834A1|1985-02-28|Process for the recovery of non ferrous and precious metals from carbon-containing materials
    DE2604164A1|1976-08-26|METHOD FOR PRODUCING SYNTHESIS GAS
    DE112009001344T5|2011-07-14|Gasification with separate calcination
    DE10121624C1|2002-10-17|Evaluating the waste heat produced from pig iron production in rotating furnaces comprises after burning a waste gas together with combustion air to form an inert process gas, forming hot vapor, and super heating the hot vapor
    DE102014209529A1|2015-11-26|Combustion of lithium at different temperatures, pressures and gas surplus with porous tubes as a burner
    EP2663661B1|2015-09-09|Method for treating a carbon dioxide-containing waste gas from an electrofusion process
    DE102013112995B4|2019-10-31|A method of heating a fuel bed in a fixed bed pressure gasification reactor
    DE102010051527A1|2012-05-16|Method for cooling steam reformer of steam reformation plant, comprises vaporizing water from boiler steam drum in waste heat boiler arranged in flue gas system of the reformer, and conducting the vapor as coolant through reformer pipes
    DE102019111827B4|2021-01-14|Method for operating a pyrolysis plant and pyrolysis plant
    CH712284A1|2017-09-29|Process for the carbothermic reduction of zinc oxide to zinc.
    CH712073A2|2017-07-31|Process for the carbothermic reduction of zinc oxide to zinc.
    DE102011002612A1|2012-07-19|Process for treating a carbon dioxide-containing exhaust gas
    AT128326B|1932-05-25|Process for reducing the specific fuel consumption and regulating the temperature in metallurgical furnaces of all kinds.
    DE102018132736A1|2020-06-18|Process and plant for producing one or more gaseous reaction products in a fired reactor
    DE112010005234T5|2013-01-24|Energy recovery from gases in a blast furnace plant
    DE102016012419A1|2018-04-19|Process for recovering heat from a flue gas produced by a burner and corresponding heat recovery system
    DE102021104000A1|2021-08-26|Method for operating incineration devices in iron and steel works, in particular integrated iron and steel works, with reduced CO2 emissions
    DE102014112629A1|2016-03-03|Process for the production of pig iron in the blast furnace and blast furnace for the production of pig iron by melting and by reduction of aufzuschmelzendem and to be reduced material
    同族专利:
    公开号 | 公开日
    CN103842759A|2014-06-04|
    AU2012228448B2|2016-08-25|
    ZA201306954B|2014-08-27|
    CA2830210A1|2012-09-20|
    CN103842759B|2016-10-12|
    AU2012228448A1|2013-10-03|
    US20140000535A1|2014-01-02|
    AT511243B1|2013-01-15|
    RU2610999C2|2017-02-17|
    WO2012123320A1|2012-09-20|
    RU2013146337A|2015-04-27|
    UA113509C2|2017-02-10|
    KR20140019389A|2014-02-14|
    BR112013023472A2|2016-12-06|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    WO2010042023A1|2008-10-06|2010-04-15|Luossavaara-Kiirunavaara Ab|Process for production of direct reduced iron|
    AT507525B1|2008-10-23|2010-09-15|Siemens Vai Metals Tech Gmbh|METHOD AND DEVICE FOR OPERATING A MELT REDUCTION PROCESS|
    AT507632A1|2008-11-21|2010-06-15|Siemens Vai Metals Tech Gmbh|METHOD AND DEVICE FOR GENERATING A SYNTHESIS OXYGEN|
    AT508522A1|2009-07-31|2011-02-15|Siemens Vai Metals Tech Gmbh|REFORMERGAS-BASED REDUCTION PROCESS WITH REDUCED NOX EMISSION|
    US3905806A|1973-02-20|1975-09-16|Armco Steel Corp|Method for the direct reduction of iron ores|
    US3844766A|1973-12-26|1974-10-29|Midland Ross Corp|Process for reducing iron oxide to metallic sponge iron with liquid or solid fuels|
    US3925190A|1974-07-29|1975-12-09|Oil Shale Corp|Preheating oil shale prior to pyrolysis thereof|
    DE2734961B2|1977-08-03|1980-02-28|Gottfried Bischoff Bau Kompl. Gasreinigungs- Und Wasserrueckkuehlanlagen Gmbh & Co Kg, 4300 Essen|Converter plant for refining steel from pig iron|
    DE2738442B2|1977-08-26|1979-10-18|Didier Engineering Gmbh, 4300 Essen|Process or system for using the sensible heat of coke in a coking system|
    US4302218A|1980-06-16|1981-11-24|Fmc Corporation|Process for controlling sulfur oxides in coal gasification|
    EP0199902A1|1985-04-29|1986-11-05|GebràœDer Sulzer Aktiengesellschaft|Combined hot air and steam plant|
    US4973528A|1990-05-10|1990-11-27|International Fuel Cells Corporation|Fuel cell generating plant|
    US5958107A|1993-12-15|1999-09-28|Bechtel Croup, Inc.|Shift conversion for the preparation of reducing gas|
    TW303389B|1994-10-17|1997-04-21|V0Est Alpine Industrieanlagenbau Gmbh|
    AT406484B|1995-08-16|2000-05-25|Voest Alpine Ind Anlagen|METHOD FOR THE PRODUCTION OF LIQUID PIG IRON OR LIQUID STEEL PRE-PRODUCTS AND SPONGE OF IRON, AND SYSTEM FOR IMPLEMENTING THE METHOD|
    AT406485B|1995-10-10|2000-05-25|Voest Alpine Ind Anlagen|METHOD FOR THE PRODUCTION OF LIQUID PIPE IRON OR LIQUID STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD|
    AT406380B|1996-03-05|2000-04-25|Voest Alpine Ind Anlagen|METHOD FOR PRODUCING LIQUID GUT IRON OR LIQUID STEEL PRE-PRODUCTS AND SYSTEM FOR IMPLEMENTING THE METHOD|
    JP3048971B2|1997-08-25|2000-06-05|川崎重工業株式会社|Exhaust heat recovery device|
    CN1502547A|1997-10-07|2004-06-09|Jfe控股公司|Catalyst for manufacturing hydrogen or synthesis gas and manufacturing method of hydrogen or synthesis gas|
    JP2001254901A|2000-03-09|2001-09-21|Daido Steel Co Ltd|Method for operating heat exchanger for waste heat recovery of exhaust gas treatment facility|
    AT409634B|2000-05-15|2002-09-25|Voest Alpine Ind Anlagen|METHOD AND DEVICE FOR THE PRODUCTION OF RAW IRON OR LIQUID STEEL PRE-PRODUCTS FROM IRON-CONTAINING MATERIALS|
    US6244200B1|2000-06-12|2001-06-12|Institute Of Gas Technology|Low NOx pulverized solid fuel combustion process and apparatus|
    CN1791686A|2003-05-15|2006-06-21|海尔萨可变资产股份有限公司|Method and apparatus for improved use of primary energy sources in integrated steel plants|
    KR101108617B1|2004-09-02|2012-01-31|재단법인 포항산업과학연구원|Combustion waste gas heat recovery system in reheating furnace|
    DE102006048600B4|2006-10-13|2012-03-29|Siemens Vai Metals Technologies Gmbh|Method and device for producing molten material|
    AT507823B1|2009-01-30|2011-01-15|Siemens Vai Metals Tech Gmbh|METHOD AND APPARATUS FOR PRODUCING RAW IRONS OR LIQUID STEEL PREPARED PRODUCTS|
    AT508770B1|2009-09-11|2011-04-15|Siemens Vai Metals Tech Gmbh|METHOD FOR REMOVING CO2 FROM EXHAUST GASES FROM PLANTS FOR THE PRODUCTION OF REFRIGERATED IRON|EP2738268A1|2012-11-29|2014-06-04|Siemens VAI Metals Technologies GmbH|Method for reduction of metal oxides to metallised material in a direct reduction process|
    US20140353886A1|2013-05-29|2014-12-04|Air Products And Chemicals, Inc.|Purification, Recovery, and Recycle of Vent Gas|
    EP3034631A1|2014-12-17|2016-06-22|Primetals Technologies Austria GmbH|Direct reduction method with gas cooling|
    CN105737123B|2016-04-15|2017-10-13|中冶华天工程技术有限公司|Blast furnace gas distributed energy resource system|
    法律状态:
    2016-06-15| PC| Change of the owner|Owner name: PRIMETALS TECHNOLOGIES AUSTRIA GMBH, AT Effective date: 20160415 |
    2018-11-15| MM01| Lapse because of not paying annual fees|Effective date: 20180317 |
    优先权:
    申请号 | 申请日 | 专利标题
    ATA368/2011A|AT511243B1|2011-03-17|2011-03-17|HÜTTENTECHNISCHE ANLAGE WITH EFFICIENT DOWNWATER USE|ATA368/2011A| AT511243B1|2011-03-17|2011-03-17|HÜTTENTECHNISCHE ANLAGE WITH EFFICIENT DOWNWATER USE|
    US14/005,658| US20140000535A1|2011-03-17|2012-03-08|Metallurgical plant with efficient waste-heat utilization|
    PCT/EP2012/053975| WO2012123320A1|2011-03-17|2012-03-08|Metallurgical plant with efficient waste-heat utilization|
    KR1020137027420A| KR20140019389A|2011-03-17|2012-03-08|Metallurgical plant with efficient waste-heat utilization|
    UAA201311033A| UA113509C2|2011-03-17|2012-03-08|METHOD OF METALLURGY INSTALLATION AND METALLURGICAL INSTALLATION|
    CN201280013726.8A| CN103842759B|2011-03-17|2012-03-08|There is the metallurgical technology device of efficient Waste Heat Reuse|
    RU2013146337A| RU2610999C2|2011-03-17|2012-03-08|Metallurgical plant with efficient use of waste heat|
    CA2830210A| CA2830210A1|2011-03-17|2012-03-08|Metallurgical plant with efficient waste-heat utilization|
    AU2012228448A| AU2012228448B2|2011-03-17|2012-03-08|Metallurgical plant with efficient waste-heat utilization|
    BR112013023472A| BR112013023472A2|2011-03-17|2012-03-08|Operation method for a metallurgical plant that has a metallurgical plant and power plant|
    ZA2013/06954A| ZA201306954B|2011-03-17|2013-09-16|Metallurgical plant with eefficient waste-heat utilization|
    [返回顶部]